RU2667519C2 - Improved reactor systems, which are catalyzed by homogeneous catalysts - Google Patents

Abstract

FIELD: chemistry; instrumentation.SUBSTANCE: invention relates to the reactors and methods for carrying out gas-liquid chemical reactions. Reactor for carrying out homogeneous catalytic reactions is described. Reactor comprises the reaction vessel, which is connected to the product outlet line, the gas spraying device, which is connected to the gas supply line, where the gas spraying device is near the bottom of the reaction vessel, and the liquid distributor, which is located near the top of the reaction vessel. Reactor further comprises the catalyst pre-conditioning system, which is connected to the liquid supply line. Method for carrying out the process is also described.EFFECT: technical result is to ensure homogeneous catalytic reactions in a new technological design.12 cl, 3 dwg

Description

Technical field

The object disclosed herein relates to reactors and methods for conducting gas-liquid chemical reactions.

State of the art

Gas-liquid chemical and biochemical reactions catalyzed by homogeneous catalysts can be carried out in some conventional reactor systems, including ideal displacement reactors (PFR), continuous stirred tank reactors (CSTR), and bubble column reactors (BCR). However, PFRs may have limited heat dissipation, which in turn requires a high flow rate. CSTRs may be characterized by low selectivity and reactor fouling. CSTRs can be characterized by relatively wide retention time distributions, which can lead to relatively high concentrations of impurities that can be difficult to remove. BCRs may be characterized by indefinite flow conditions in the reactor and inhomogeneous mixing, which can cause low selectivity and difficulties in large scale implementation.

Thus, there remains a need in the art for improved reactors and methods for reactions with improved properties catalyzed by homogeneous catalysts, including stirring, heat removal, efficiency and selectivity.

SUMMARY OF THE INVENTION

In various embodiments, reactors and process methods are disclosed.

A reactor for carrying out processes for a product withdrawal line comprises: a reaction vessel adapted to be connected to a product withdrawal line; a gas sprinkler adapted to be connected to a gas supply line; and a liquid distributor located near the upper part of the reaction vessel and adapted to be connected to a liquid supply line.

The method of the process includes: providing a reactor containing a reaction vessel; supplying gas to the reaction vessel through a gas sprayer connected to the reaction vessel and a gas supply line; supplying liquid to the reaction vessel through a liquid distributor located near the top of the reaction vessel and connected to a liquid supply line; carrying out the reaction in the reaction vessel and withdrawing the product from the reaction vessel through a product withdrawal line connected to the reaction vessel.

These and other features and characteristics are described in more detail below.

Brief Description of the Drawings

The following is a brief description of the graphic materials in which such elements are numbered identically and which are presented for the purpose of illustrating the typical embodiments disclosed herein, and not for the purpose of limiting them.

FIG. 1 is a schematic diagram depicting a typical reactor according to one non-limiting embodiment of the disclosed object.

FIG. 2A is a schematic diagram depicting another exemplary reactor according to one non-limiting embodiment of the disclosed subject.

FIG. 2B is a circuit diagram further illustrating the reactor of FIG. 2A.

DETAILED DESCRIPTION OF THE INVENTION

The object disclosed herein provides reactors and methods for conducting gas-liquid chemical reactions.

The object disclosed herein provides reactors and processes for carrying out processes, including but not limited to homogeneous catalytic gas-liquid chemical reactions. According to one embodiment, a typical process reactor for a product withdrawal line may comprise a reaction vessel adapted to be connected to the product withdrawal line. The reactor may also comprise a gas sprinkler adapted to be connected to the gas supply line and a liquid distributor located near the top of the reaction vessel. The liquid distributor may be adapted to be connected to a liquid supply line.

According to some embodiments of the disclosed object, a gas sparger may be designed to provide gas through a plurality of (for example, more than 1) places along the sides of the reactor. Additionally or alternatively, the gas spray may be located near the bottom of the reaction vessel.

In some embodiments of the disclosed object, the reactor may further comprise a stirrer. The mixer may be located near the bottom of the reaction vessel.

According to some embodiments of the disclosed object, a catalyst preforming system may be coupled to a liquid supply line. A catalyst pre-forming system may be designed to dispense one or more catalyst solutions.

In some embodiments of the disclosed object, the reactor may further comprise a mist eliminator located near the top of the reaction vessel. The mist eliminator may include a removable mist eliminator.

In some embodiments of the disclosed object, the reactor may further comprise a jacket designed to circulate a heating or cooling medium therethrough. The jacket may be designed to provide heat or to remove heat from the reaction vessel.

According to some embodiments of the disclosed object, the product withdrawal line may be connected to a separation system. A separation system can be designed to purify the desired product.

In some embodiments of the disclosed object, the reactor may further comprise thermocouples at a plurality of locations in the reactor.

According to some embodiments of the disclosed object, the reaction vessel may further comprise a sight glass. The sight glass can be designed to control the reaction vessel, including monitoring the reaction carried out in the reactor, monitoring the dosing of the feed to the reactor, monitoring the mixing circuit in the reactor and / or monitoring the product properties in the reactor.

In some embodiments of the disclosed object, a reactor may be designed to conduct oligomerization reactions. For example, a reactor may be designed to oligomerize ethylene into one or more of 1-butene, 1-hexene, 1-octene, or a combination comprising at least one of the foregoing.

In some embodiments of the disclosed object, the reactor does not comprise a cooling coil.

The object disclosed herein may also provide processes, including but not limited to homogeneous catalytic gas-liquid chemical reactions. In one embodiment, a typical process method may include providing a reactor containing a reaction vessel. The method may also include supplying gas to the reaction vessel through a gas sparger connected to the reaction vessel and the gas supply line. The method may also include supplying liquid to the reaction vessel by means of a liquid distributor located near the top of the reaction vessel and connected to a liquid supply line. The method may also include carrying out the reaction in a reaction vessel. The method also includes discharging the product from the reaction vessel through a product discharge line connected to the reaction vessel.

According to some embodiments of the disclosed object, the process may be a homogeneous catalytic process. In some embodiments of the disclosed subject, the reaction may include one or more oligomerization reactions. For example, oligomerization reaction (s) may include ethylene oligomerization into one or more of 1-butene, 1-hexene, 1-octene, or a combination comprising at least one of the foregoing. The product may include one or more of 1-butene, 1-hexene, 1-octene, or a combination comprising at least one of the foregoing.

For purposes of illustration, and not limitation, FIG. 1, 2A and 2B are schematic views of a typical reactor according to the disclosed object. The reactor 100, 200 may comprise a reaction unit or vessel 101, 201 with a reaction chamber 102, 202 therein. The reactor 100, 200 may consist of any desired materials, for example, including, but not limited to, metals, alloys, including steel, glass, enamels, ceramics, polymers, plastics, or a combination comprising at least one of the foregoing. The reactor 100, 200, the reaction vessel 101, 201 and the chamber 102, 202 can be of any desired design or shape, for example, including, but not limited to, tubular, cylindrical (as shown in Figs. 1, 2A and 2B), rectangular, domed or cone-shaped. The dimensions and size of the reactor 100, 200, the reaction vessel 101, 201 and the chamber 102, 202 may depend on the desired type of reaction, productivity, type of feed and any catalyst for which the reactor is intended. For example, the size of the reaction vessel can range from about 50 milliliters (ml) (for example, for laboratory reactors) to about 20,000 liters (l) (for example, for industrial reactors). The ratio of height to width of the reaction vessel 101, 201 may vary. For example, the ratio of height to width of the reactor 100, 200 and the reaction vessel 101, 201 may be from about 0.5: 1 to about 10: 1. In some embodiments, where the reactor 100, 200 and the reaction vessel 101, 201 are cylindrical, the ratio of height to width can also be expressed as the ratio of height to diameter. The geometric dimensions of the reactor 100, 200, the reaction vessel 101, 201 and the chamber 102, 202 can be adjusted in various ways.

The reactor 100, 200 may include a mixer 103, and / or one or more blades 104, and / or one or more deflectors 105. The reactor 100, 200 may contain one or more samplers. The stirrer, blade (s) and deflector (s) can be made of any desired materials and arranged in any desired configuration. For example, the agitator 103 may be a paddle agitator, an anchor agitator, a propeller agitator, a radial propeller agitator, a turbine agitator or a screw agitator. The stirrer 103 may be coupled via a shaft to the vane (s) 104. More than one vane 104 may be connected to the agitator 103 at various locations along the agitator 103. The agitator 103 may be located near the bottom of the reaction vessel. For example, the stirrer 103 may be located in the lower part of the reaction vessel or in the range of about 10% to about 25% of the distance from the lower part of the reaction vessel to the upper part of the reaction vessel 101. The blade (s) 104 may be single-blade, two-blade, or any other desired blade (yami). The deflector (s) 105 may take the form of a wall mounted device or may have other suitable constructions known to one skilled in the art, such as a longitudinal flow deflector, a deflector with holes, a single segment deflector or a two segment deflector. The baffle (s) can accelerate mixing and improve heat transfer in the reactor.

The reactor 100, 200 may contain both a stirrer 103 and a gas sprinkler 106, 206. A gas sprinkler 106, 206 may be designed to provide gas through multiple locations along the sides of the reactor. Additionally or alternatively, the gas sparger 106, 206 may be located near the bottom of the reaction vessel for supplying gas from the bottom of the reactor. For example, a gas sparger 106, 206 may be in the lower part of the reaction vessel or in the range of about 10% to about 25% of the distance from the lower part of the reaction vessel 101, 201 to the upper part of the reaction vessel 101, 201.

The gas sprinkler 106, 206 may be adapted to be connected to the gas supply line 111, 211. The gas sprinkler 106, 206 may be a stationary sprinkler. The gas sprinkler 106, 206 may be a one-piece sprinkler, or a two-piece sprinkler.

The gas supply line 111, 211 may be connected to a gas source 112, 212, for example, gas cylinders. Gaseous feedstocks may include, but are not limited to, reagents, reagents, catalysts, cocatalysts, initiators, oxidizing agents, reducing agents, solvents, or a combination comprising at least one of the foregoing. For example, the gaseous feed may contain olefinic compounds, including but not limited to ethylene. The gaseous feed may include hydrogen gas. Hydrogen gas can help reduce polymer pollution.

The combination of a stirrer 103 and a gas sprayer 106, 206 can provide advantages for both a continuous stirred tank reactor (CSTR) and a bubble column reactor (BCR) and improve mixing compared to previously existing methods. The combination of a stirrer 103 and a gas sprinkler 106, 206 can improve the efficiency, selectivity and other properties of reactions that are limited by diffusion. The combination of a stirrer 103 and a gas sprayer 106, 206 can reduce temperature gradients in the reaction vessel, which can improve the quality and purity of the reaction products.

The reactor 100, 200 can be heated or cooled by an external jacket 107, 207 mounted on or near the reactor. The jacket 107, 207 may be of any desired design for circulating a heating or cooling medium, and may be made of any desired material.

The jacket 107, 207 can control the temperature of the reaction carried out in the reaction chamber by circulating a working fluid that acts as a heating medium and / or cooling medium through the inlet of the shirt 108, 208 and the shirt outlet 109, 209. For example, working fluids may include DOWTHERM ™, THERMINOL®, SYLTHERM ™, other silicone oils, water, organic oils, glycols (e.g. ethylene glycol and propylene glycol) and similar fluids, as well as mixtures and combinations containing at least one of the foregoing. According to some non-limiting embodiments, the temperature of the working fluid used as a cooling medium may be from about -110 ° C to about 20 ° C.

The use of a jacket 107, 207 can help control and regulate the temperature of the reactor 100, 200 and the reaction vessel 101, 201. Monitoring and controlling the temperature of the reactor and the reaction vessel can be important, for example, when the process is exothermic or endothermic.

The gas supplied through the gas sprinkler 106, 206 can also help to remove heat from the reactor and cool the reaction vessel. Thus, in the reactor, it is possible to provide dual modes of cooling, using both the outer jacket 107, 207 and gas sparging to provide improved heat removal from the system. Efficient heat removal from the reactor can help prevent thermal instability. Therefore, the reactor 100, 200 may contain a cooling coil, but does not require it.

The reactor 100, 200 may include a liquid distributor 114, 214 and a liquid supply line 110, 210. The liquid distributor 114, 214 may be located near the top of the reaction vessel 101, 201 and be adapted to be connected to the liquid supply line 110, 210. For example, a liquid distributor 114, 214 may be located in the upper part of the reaction vessel or in the range of from about 20% to about 35% of the distance from the upper part of the reaction vessel 101, 201 to the lower part of the reaction vessel 101, 201. Via a liquid supply line 110, 210 and through a liquid distributor 114, 214, liquids may be supplied to the reaction vessel. The liquid feed may be suitably diluted or concentrated liquid known to a person skilled in the art. Liquid feeds may include, but are not limited to, reagents, reagents, catalysts, cocatalysts, initiators, oxidizing agents, reducing agents, solvents, or a combination comprising at least one of the foregoing. Non-limiting examples of liquid feeds may include hydrocarbon solvents, for example, toluene, hexanes, cyclohexanes, or a combination comprising at least one of the foregoing. Although one fluid supply line 110, 210 is shown in FIG. 1 and 2, a plurality of fluid supply lines can be used.

According to some embodiments of the disclosed object, the liquid supply line 110, 210 may include one or more drying filters. Drying filters can remove water.

The reactor 100, 200 may comprise a plurality of thermocouples 113, 213 located at various places in the reactor. Thermocouples can be designed to evaluate kinetics. For example, thermocouples can be designed to help control the operation of a reactor system by detecting errors in flow distribution, channel formation, and other events. Thermocouples can be multi-point thermocouples. Thermocouples can be connected to the reactor by suitable methods known to a person skilled in the art, for example, using Pt-100 compounds. The compounds may be wire, thin film and / or reel.

The reactor 100, 200 may comprise a catalyst pre-forming system 115, 215. The catalyst pre-forming system may be connected to a liquid supply line 110, 210. Alternatively, the catalyst pre-forming system may be connected to a reactor 100, 200 and a reaction vessel 101, 201 without being connected to a liquid supply line 110, 210. The catalyst pre-forming system 115, 215 can dispense a single catalyst solution. Alternatively, in some embodiments of the disclosed subject, a catalyst pre-forming system 115, 215 may combine two or more catalyst solutions or pre-catalysts. In some preferred embodiments, the catalyst pre-forming system 115, 215 may combine two or three solutions of the catalysts or pre-catalysts. The catalyst pre-forming system 115, 215 may combine two or more catalyst solutions or pre-catalysts to provide a combined catalyst solution. When the catalyst is supplied to the reaction vessel 101, 201, various reactions can be catalyzed.

The reactor 100, 200 may comprise a mist eliminator 116, 216. According to some embodiments of the disclosed object, the mist eliminator 116, 216 may be located near the top of the reaction vessel 101, 201. For example, the mist eliminator 116, 216 may be located at the top of the reaction vessel or in the range of approximately 10% to approximately 25% of the distance from the upper part of the reaction vessel to the lower part of the reaction vessel 101, 201. The mist eliminator 116, 216 may be a removable mist eliminator. In some embodiments, the mist eliminator 116, 216 may be a wire mesh mist eliminator. A mist eliminator 116, 216 can allow vapors to pass through it while collecting liquid droplets and causing liquid to drip into the reaction vessel 101, 201. In some embodiments, the mist eliminator 116, 216 can collect liquid droplets with a particle size of from about 10 micrometers to about 100 micrometers. The mist eliminator 116, 216 can be used when the reactor 100, 200 does not contain a stirrer 103.

The reactor 100, 200 may comprise a product withdrawal line 117, 217 connected to the reactor. A product withdrawal line 117, 217 is connected to a reactor 100, 200 for withdrawing products from the reaction vessel 101, 201. Although one product withdrawal line 117 is shown in FIG. 1, a plurality of product withdrawal lines 217 may be used as shown in FIG. 2. The product withdrawal line 117, 217 may be located on the side of the reaction vessel, in the lower part of the reaction vessel and / or in other places on the reaction vessel. The product withdrawal line 117, 217 may comprise one or more samplers, as shown in FIG. 2. According to some embodiments of the disclosed object, the product withdrawal line 117, 217 may also be connected to a separation system 118, 218. Separation system 118, 218 can be used to purify reactor effluent and to separate reactor effluent into various valuable products. For example, separation system 118, 218 can be used to cool one or more catalysts according to techniques known to one skilled in the art.

The reactor 100, 200 may comprise a sight glass 119, 219. The sight glass 119, 219 may be at an angle of 180 degrees to the vertical axis of the reactor 100, 200. The sight glass 119, 219 can be used for various purposes, including, but not limited to, monitoring the conditions inside reaction vessel 101, 201. The sight glass 119, 219 can be designed to control the reaction carried out in the reactor, control the dosing of the feed to the reactor, control the mixing circuit in the reactor and / or control the product properties in the reactor.

According to some embodiments of the disclosed object, the reactor 100, 200 may operate in continuous mode or semi-continuous mode. The reactor 100, 200 may also operate in a batch mode, for example, by shutting off the product line (s) 117, 217. The disclosed reactor 100, 200 can operate at various pressures and temperatures. In some non-limiting embodiments, the pressure in the reactor 100, 200 and in the reaction vessel 101, 201 may be from about 1 megapascal (MPa) to about 12 MPa (from about 10 bar to about 120 bar). In some preferred embodiments, the pressure may be from about 2 MPa to about 7 MPa (from about 20 bar to about 70 bar). According to some non-limiting embodiments, the temperature in the reactor 100, 200 and in the reaction vessel 101, 201 may be from about 30 ° C to about 70 ° C. Operating temperature and pressure may depend on the process requirements for the desired reaction.

The reactor 100, 200 can be designed to carry out one or more catalytic reactions, such as oxidation, hydrogenation, condensation, alkylation, etc. The reactor can be used to carry out homogeneous catalytic endothermic or exothermic processes to produce any desired chemicals, polymers, petrochemical products, agrochemicals and / or drugs. In some embodiments of the disclosed subject, oligomerization reactions can be carried out. For example, olefin feedstocks, such as ethylene, may be the basis for oligomerization. Ethylene can be oligomerized to produce higher olefins, such as 1-butene, 1-hexene, 1-octene, 1-decene, 1-dodecene and higher olefins.

The reactor 100, 200 may also contain any devices known to a person skilled in the art, including but not limited to measuring devices, heating elements, pH indicators, densitometers and viscometers. The reactor 100, 200 may also comprise any suitable safety device, including but not limited to a bursting diaphragm, pressure relief valves (PSV) and / or gas detectors (for example, detectors for carbon monoxide, oxygen, hydrogen and ammonia). Typical measuring devices may be any measuring devices known to one skilled in the art. For example, measurement devices may include, but are not limited to, pressure indicators, pressure sensors, thermowells, temperature indicator controllers, and analyzers. These devices can be placed in various places on the reactor, for example, on the walls or in the upper part of the reactor or near it. The reactor 100, 200 may contain various safety devices and means known to a person skilled in the art for reducing temperatures and / or pressures that are too high. These safeguards can thereby eliminate and / or control thermal instability.

The object disclosed herein may also provide processes, including but not limited to homogeneous catalytic gas-liquid chemical reactions. In one embodiment, a typical process method may include providing a reactor 100, 200 comprising a reaction vessel 101, 201. Gas may then be supplied to the reaction vessel 101, 201 through a gas sprinkler 106, 206 connected to a gas supply line 111, 211 that may be further connected to a gas source 112, 212. Liquid can be supplied to the reaction vessel 101, 201 by means of a liquid distributor 114, 214 connected to a liquid supply line 110, 210. The reaction can be carried out in the reaction vessel 101, 201. The reaction products can be withdrawn from the reaction vessel 101, 201 through one or more product withdrawal lines 117, 217 connected to the reaction vessel.

According to some embodiments of the disclosed object, the process may be a homogeneous catalytic process. According to some embodiments of the disclosed object, one or more catalyst solutions for initiating a gas-liquid chemical reaction can be supplied to the reaction vessel 101, 201 from the catalyst pre-forming system 115, 215, which can be connected to the liquid supply line 110, 210 or alternatively, connected directly to the reaction capacity of 101, 201.

In some embodiments of the disclosed subject, the reaction may include one or more oligomerization reactions. Oligomerization reactions may include ethylene oligomerization to one or more of 1-butene, 1-hexene, 1-octene, or a combination containing at least one of the foregoing. Methods for conducting homogeneous catalytic processes may include feeding gaseous ethylene into the reaction vessel 101, 201 through a gas sprinkler 106, 206, allowing ethylene to oligomerize under homogeneous catalytic conditions, and withdrawing one or more of 1-butene, 1-hexene, 1-octene, or a combination containing at least one of the above, as a reaction product (s) via a product withdrawal line 117, 217 connected to the reaction vessel. The selectivity of ethylene oligomerization may depend on the nature of the catalyst system used. Various catalyst systems can facilitate the oligomerization of ethylene to produce 1-butene, 1-hexene, 1-octene, 1-decene, 1-dodecene and / or higher olefins. For example, catalytic systems may be sensitive to traces of impurities in the feed and / or reaction liquids. Such impurities can alter the nature of the catalyst systems and can in some cases contribute to the formation of undesirable by-products relative to the desired products.

The reactors and methods disclosed herein include at least the following embodiments.

Embodiment 1: A process reactor for a product withdrawal line, comprising: a reaction vessel adapted to be connected to a product withdrawal line; a gas sprinkler adapted to be connected to a gas supply line; and a liquid distributor located near the upper part of the reaction vessel and adapted to be connected to a liquid supply line.

Embodiment 2: The reactor of claim 1, wherein the gas sparger is designed to provide gas through multiple locations along at least one side of the reactor.

Embodiment 3: A reactor according to claim 1 or claim 2, wherein the gas sprayer is located near the bottom of the reaction vessel.

Option exercise 4: The reactor according to any one of paragraphs. 1-3, and the reactor further comprises a stirrer.

Embodiment 5: The reactor of claim 4, wherein the stirrer is located near the bottom of the reaction vessel.

Option exercise 6: The reactor according to any one of paragraphs. 1-5, further comprising a catalyst pre-forming system coupled to the liquid supply line.

Embodiment 7: The reactor of claim 6, wherein the catalyst pre-forming system is designed to dispense one or more catalyst solutions.

Option exercise 8: The reactor according to any one of paragraphs. 1-7, further comprising a mist eliminator located near the top of the reaction vessel.

Embodiment 9: The reactor of claim 8, wherein the mist eliminator comprises a removable mist eliminator.

Option exercise 10: The reactor according to any one of paragraphs. 1-9, further comprising a jacket connected to the reactor and designed to circulate a heating or cooling medium therethrough.

Embodiment 11: The reactor of claim 10, wherein the jacket is designed to provide heat or to remove heat from the reaction vessel.

Option exercise 12: The reactor according to any one of paragraphs. 1-11, in which the product withdrawal line is connected to a separation system.

Option exercise 13: The reactor according to any one of paragraphs. 1-12, further comprising thermocouples at a variety of locations in the reactor.

Option exercise 14: The reactor according to any one of paragraphs. 1-13, in which the reaction vessel contains a sight glass.

Embodiment 15: The reactor of claim 14, wherein the sight glass is designed to control one or more reactions carried out in the reactor, dispense the feed into the reactor, stirring schemes in the reactor, and product properties in the reactor.

Option exercise 16: The reactor according to any one of paragraphs. 1-15, and the reactor is designed to conduct oligomerization reactions.

Embodiment 17: A process method comprising: providing a reactor comprising a reaction vessel; supplying gas to the reaction vessel through a gas sprayer connected to the reaction vessel and a gas supply line; supplying liquid to the reaction vessel through a liquid distributor located near the top of the reaction vessel and connected to a liquid supply line; carrying out the reaction in the reaction vessel and withdrawing the product from the reaction vessel through a product withdrawal line connected to the reaction vessel.

Embodiment 18: The method of claim 17, wherein the process is a homogeneous catalytic process.

An implementation option 19: The method according to p. 17 or p. 18, in which the reaction includes an oligomerization reaction.

Option exercise 20: The method according to any one of paragraphs. 17-19, in which the product contains one or more of 1-butene, 1-hexene, 1-octene, or a combination containing at least one of the above.

As used herein, the expression “approximately” or “approximately” means within the margin of error for a particular value determined by a person skilled in the art, which will depend in part on how the value is measured or determined, i.e. limitations of the measurement system. For example, “approximately” may mean a range of up to 20%, up to 10%, up to 5% and / or up to 1% of a given value.

Although the object disclosed herein and its advantages have been described in detail, it should be understood that various changes, substitutions and variations can be made in this document without deviating from the essence and scope of the disclosed object defined by the attached claims. In addition, the scope of the disclosed object is not intended to be limited to the specific embodiments described in the description. As one skilled in the art will readily appreciate from the disclosure of the disclosed subject matter, alternatives already existing or developed later that perform substantially the same function or achieve substantially the same result as the corresponding embodiments described herein can be used according to the subject disclosed herein. Therefore, the appended claims are intended to include such alternatives within their scope.

A more complete understanding of the components, processes and devices disclosed in this document can be achieved with reference to the attached graphic materials. These figures (also referred to herein as “figures.”) Are only schematic views for the convenience and simplicity of the image of the present disclosure and, therefore, are not intended to indicate the relative size and dimensions of the devices or their components and / or to determine or limit the scope of typical options for implementation. Although specific expressions are used in the following description for clarity, these expressions are intended to refer only to the specific structure of the embodiments selected for illustration in the figures, and are not intended to define or limit the scope of the present disclosure. Regarding the figures and the following description, it should be understood that such numerical designations refer to components with a similar function.

In general, the present invention may alternatively comprise, consist of, or consist essentially of any suitable components disclosed herein. The present invention may additionally or alternatively be formulated so as not to contain or essentially not contain any components, materials, ingredients, excipients or products used in the compositions of the prior art or which in other cases are not necessary to achieve the function and / or objectives of the present invention. The endpoints of all ranges related to the same component or property are inclusive and independently combined (for example, ranges less than or equal to 25 wt.%, Or from 5 wt.% To 20 wt.% Are inclusive of endpoints and all intermediate values of the ranges "From 5 wt.% To 25 wt.%", Etc.). The disclosure of a narrower range or a more specific group in addition to a wider range is not a negation of a wider range or a larger group. A “combination” is including combinations, mixtures, alloys, reaction products and the like. In addition, the expressions “first”, “second” and the like in this document do not mean any order, quantity or importance, but rather are used to distinguish one element from another. Expressions in the singular in this document do not mean a limitation of quantity and should be considered as covering both singular and plural forms, unless otherwise indicated in this document or is clearly contrary to the context. “Or” means “and / or”. The plural suffix, as used herein, is intended to include both the singular and plural forms of the expression that it modifies, thus including one or more such expressions (for example, film (s) includes one or more films). The reference throughout the description to “one embodiment”, “another embodiment”, “embodiment”, etc. means that a particular element (eg, feature, structure, and / or characteristic) described with respect to an embodiment is included in at least one embodiment described herein and may or may not be present in other embodiments. In addition, it should be understood that the described elements can be combined in any suitable manner in various embodiments.

The “approximately” modifier used in relation to quantity is inclusive of the indicated value and has a value determined by the context (for example, includes the degree of error associated with measuring a specific quantity). The designation "± 10%" means that the specified measurement can be from an amount that is minus 10% to an amount that is plus 10% of the specified value. The expressions “front”, “rear”, “lower” and / or “upper” are used herein, unless otherwise indicated, for convenience of description only and not limited to any one position or orientation in space. “Optional” or “optional” means that the event or condition described in the next step may or may not occur, and that the description includes instances where the event occurs and instances where not. Unless otherwise indicated, the technical and scientific expressions used herein have the same meaning as is commonly understood by one of ordinary skill in the art to which this invention pertains. A “combination” is including combinations, mixtures, alloys, reaction products and the like.

All cited patents, patent applications, and other references are incorporated herein by reference in their entirety. However, if the expression in this application conflicts with or conflicts with the expression in the included link, the expression from this application takes precedence over the contradictory expression from the included link.

Although specific embodiments have been described, alternatives, modifications, options, improvements, and substantial equivalents that are or may be currently unforeseen may arise with applicants or those skilled in the art. Therefore, the appended claims, as filed and how they can be changed, are intended to include all such alternatives, modifications, options, improvements, and substantial equivalents.

Claims (22)

1. A reactor for conducting homogeneous catalytic chemical reactions, containing: a reaction vessel connected to a product withdrawal line; a gas sprayer connected to a gas supply line, where the gas sprayer is located in the lower part of the reaction vessel; and a liquid distributor located near the upper part of the reaction vessel and connected to a liquid supply line; wherein the reactor further comprises a catalyst pre-forming system coupled to a liquid supply line, wherein the catalyst pre-forming system is designed to dispense one or more catalyst solutions. 2. The reactor according to claim 1, in which the gas spray is designed to provide gas through many places along at least one side of the reactor. 3. The reactor according to claim 1 or 2, in which the gas spray is located near the bottom of the reaction vessel. 4. The reactor according to any one of paragraphs. 1, 2, wherein the reactor further comprises a stirrer, and wherein the stirrer is located near the bottom of the reaction vessel. 5. The reactor according to any one of paragraphs. 1, 2, further comprising a mist eliminator located near the top of the reaction vessel, where the mist eliminator includes a removable mist eliminator. 6. The reactor according to any one of paragraphs. 1, 2, further comprising a jacket connected to the reactor and designed to circulate a heating or cooling medium therethrough, where the jacket is designed to provide heat or to remove heat from the reaction vessel. 7. The reactor according to any one of paragraphs. 1, 2, in which a product discharge line is connected to a separation system. 8. The reactor according to any one of paragraphs. 1, 2, further comprising thermocouples at a plurality of locations in the reactor. 9. The reactor according to any one of paragraphs. 1, 2, in which the reaction vessel contains a sight glass, where the sight glass is designed to control one or more reactions carried out in the reactor, dispensing the feed into the reactor, mixing schemes in the reactor and product properties in the reactor. 10. A method for conducting homogeneous catalytic chemical reactions, comprising: providing a reactor containing a reaction vessel; supplying gas to the reaction vessel through a gas sprayer connected to the reaction vessel and a gas supply line, where the gas sprayer is located at the bottom of the reaction vessel; supplying liquid to the reaction vessel through a liquid distributor located near the top of the reaction vessel and connected to a liquid supply line; supplying one or more catalyst solutions from a catalyst pre-forming system connected to a liquid supply line carrying out the reaction in the reaction vessel and product withdrawal from the reaction vessel through a product withdrawal line connected to the reaction vessel. 11. The method according to p. 10, in which the reaction includes an oligomerization reaction. 12. The method according to any one of paragraphs. 10, 11, in which the product contains one or more of: 1-butene, 1-hexene, 1-octene, or a combination containing at least one of the above.

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